Dynamically balanced multi-path liquid-gas contacting



Sheet of 2 H. E. SHOBE DYNAMICALLY BALANCED MULTI-PATH LIQUID- GAS CONTACTING a 8 mm am we a u 3 I, w\\ a Tm SA 8 mm 4 VS b 9n 4 u N QNJUNN FN -0N Nm MM\ m mw a 5 H m wh If m 7. 2 r mm i I A W J fiwa u t T: 2 m. L T: MGR hut y 4 wwzlllihkllllumlllll m URN! r F F .u 6R 'I l I I l I I I i m. w m .4 m1 9k m U? .2

May 20, 1969 Filed June 8, 1964 W W 'W ATTORNEYS I H. E. S'HOBE May 20, 1969 DYNAMICALLY BALANCED MULTI-PATH LIQUID-GAS CONTACTING Sheet 3 of 2 Filed June 8. 1964 INVENTOR. H E SHOBE (78 1 WT 4H7? A TTORNEYS United States Patent 3,445,094 DYNAMICALLY BALANCED MULTI-PATH LIQUID-GAS CONTACTING Henry E. Shobe, Bartlesville, Okla., assignor to Phillips Petroleum Company, a corporation of Delaware Filed June 8, 1964, Ser. No. 373,363 Int. Cl. B01d 3/22 US. Cl. 261114 3 Claims ABSTRACT OF THE DISCLOSURE A gas and liquid contact column having a multiplicity of multi-path contacting trays with two zones of unequal areas. The trays have a plurality of downcomers dividing said trays into equal flow paths. Baflle means are provided with a plurality of separate flow openings spaced along the bafile means and proportional to the zones of unequal areas being fed by the respective downcomer.

This invention relates to liquid-gas contacting. In one aspect, it relates to liquid-gas contacting apparatus comprising multi-path contacting tray-s. In another aspect it relates to fractional distillation.

Liquid-gas contacting is involved in such liquid-gas transfer systems as, for example, distillation, rectification, absorption, stripping, humidification, dehumidification, dephlegmation, etc. For large capacity liquid-gas contacting installations, there are economic advantages in using large capacity contact vessels.

For example, for large capacity fractional distillation installations there are economic advantages in using one or more large diameter columns rather than a larger number of parallel smaller diameter columns. However, for simple two-path trays, as the column diameter is increased, a point is reached at which the horizontal liquid cross-flow paths become too long for stable operation. This occurs due to the sloping liquid surface which exists in order to supply the energy necessary to drive the liquid across the flow path. When the length of the flow path is excessive, a sufficient variation in head of liquid exists across the tray that upfiowing vapor flows in greater quantity near the liquid discharge side of the flow path where the head of liquid is smallest. The excessive vapor flow in this area entrains liquid and, as the vapor redistributes itself across the column, tends to move the liquid toward a point of higher head, thus aggravating the imablance. Unstable tray operation and column flooding result. The exact diameter of column for which length of flow path becomes a serious problem varies with the density of the liquid and other parameters, but, for many of the common lighter hydrocarbon separations, the longest flow path which can be used efiiciently often is of the order of four feet in length.

Multi-path trays can avoid the problems occasioned by long flow paths. By multi-path tray as used herein is meant one which has three or more separate liquid flow paths between tray inlets and tray outlets. This concept is distinguished from dividing liquid flow into several portions across a single tray path. As used herein, there- 'ice fore, a path is a portion of a tray over which liquid flows substantially in a single direction from a tray inlet to a tray outlet. On adjacent paths the flow is substantially in opposite directions, either from separate spaced inlets to a common outlet, or from a common inlet to separate outlets. The desired result is to attain shorter flow path lengths. However, with multi-path trays I have found that the column operation is diflicult to balance, that is, to properly apportion liquid flows in particular, and that imbalance can be as detrimental to stable operation as long flow paths.

An objection of this invention is to contact fluids efliciently.

Another object of this invention is to provide balanced operation of a liquid-gas contacting column having multipath trays.

Another object of this invention is to determine the physical proportions of the various internal components of a liquid-gas contacting column for dynamically balanced operation.

Another object of this invention is to provide eflicient liquid-gas contacting apparatus.

Another object of this invention is to separate fluids efficiently by fractional distillation.

Other aspects, objects and the advantages of my invention are apparent in the written description, the drawing and the claims.

I have found that for balanced operation and highest contacting efficiency of a liquid-gas contacting column having multi-path trays, the following factors should be equal on the several sections of a given tray:

( l) The corresponding vertical dimensions of the tray sections are made equal.

(2) The tray section flow paths are equal in length.

(3) The horizontal dimensions of weir and downcomer lengths of the tray sections are proportioned to effect equal flow per unit of tray section area and equal liquid height on tray sections and in downcomers.

(4) Flow paths are equal by positioning downcomers to drain equal horizontal lengths of the tray.

Gas-liquid ratio Gas-liquid contact time Gas-liquid disengaging time Gas velocities Liquid velocities Gas rate per unit of active area.

Although the total horizontal length of each weir and corresponding downcomer is fixed by the length of tray across which each extends, according to my invention the effective length can be shortened by using vertical baflles along a part of the length. By unequal baflling of downcomers which distribute liquid in two directions to unequal areas, the flow can be proportioned to the areas. The height of liquid on a tray is controlled by baflling the Weirs. Since the flow over a weir is proportional to the effective length and height of liquid, when the effective length is shortened the height is increased. This efiect is utilized according to my invention to make the height of liquid on various portions of a tray equal.

As noted above, the distribution of liquid among the several tray sections is controlled by unequal downcomer bafiling. The liquid holdup in the downcomers is determined by the total bafiling on the downcomers. In this way the heights of liquid on the trays in the several downcomers and in the disengaging spaces above the liquid levels are controlled.

In all instances, adjacent baffles preferably are alternated, that is, the bafile area on one side is opposite an open area on the other side, to give maximum improvement in preventing undesired splash and blow efiects.

My invention is applicable to all multi-path trays using any of the known types of contacting means.

In the drawing:

FIGURE 1 is a schematic horizontal cross section of a four-path liquid-gas contacting column according to my invention.

FIGURES 2, 3, 4, S and 6 are schematic partial vertical cross sections of the column of FIGURE 1.

FIGURE 7 is a schematic horizontal cross section of a three-path liquid-gas contacting column according to my invention,

FIGURES 8, 9, 10 and 11 are schematic partial vertical cross sections of the column of FIGURE 7.

In the apparatus of FIGURE 1, there are four flow paths, a, b, c, d, making this a four-path design. Referring to FIGURE 1 and FIGURE 2, on tray A, path d is from downcomer 11 over weir 12, path c is from downcomer 11 to weir 13, path b is from downcomer 14 to weir 16 and path a is from downcomer 14 to weir 17.

On tray B, path a is from downcomer 18 to weir 19, path b is from downcomer 21 to weir 22, path is from downcomer 21 to weir 23 and path d is from downcomer 24 to weir 26. Similarly, on tray C, path a is from downcomer 27 to Weir 28, path b from downcomer 27 to weir 29, path 0 from downcomer 31 to weir 32, and path d from downcomer 31 to weir 33. On tray D, path a is from downcomer 34 to weir 36, path b from downcomer 37 to weir 38, path 0 from downcomer 37 to weir 39, and path d from downcomer 41 to weir 42. Each of trays A, B, C and D are spaced from adjacent trays by the same distance. Paths a, b, c and d are equal in length. Referring to tray C, it is seen that the area over which fiow path 0 extends is smaller than the area over which flow path b extends. Although the edge 27a of downcomer 27 is shorter than the edge 27b the lengths of these edges still are not in proportion with the areas fed by each. Therefore, edge 27a is partially baflled, as illustrated in FIGURE 4, while the edge 27b is unbafiled, as illustrated in FIGURE 5, so that the flow of liquid to the areas is in proportion to the areas themselves. That is, the unbafiled portion at edge 27a is in the same proportion to the area within flow path a as the length under edge 27b is to the are-a within flow path b. The two sides of downcomer 31 are similarly bafiled to feed areas 0 and d.

Although the flow is thus proportioned to the areas, the depth of liquid on the tray C, over the paths a and b, is determined by the height of liquid flowing over the Weirs 28 and 29. Since weir 29 is longer than the unbaffied area under edge 27b, while weir 28 is shorter than the unbaffied area under 27a, it is necessary to supply bafiling for weir 29 to equalize the spread of fluid over the tray A. This is illustrated in FIGURE 6.

Although the areas under flow paths b and c are equal and, therefore, the two sides or edges of downcomer 37 are equal, this downcomer is baflied, as illustrated in FIGURE 6, to control the flow to tray D so that the head of liquid held within downcomer 37 is equal to the head of liquid held within downcomers 34 and 41, which are unbaffled. Weir 36 and corresponding weir 42 are baffled in the same manner as weir 19 shown in FIGURE 4 so that the height of liquid on tray D over the areas for flow paths b and c is equal to the height over the areas for flow paths a and b. Similar baflling is provided for subsequent and preceding trays within the column.

In FIGURE 7, illustrating a three path column, flow paths e, f and g are equal in length. Flow path e on tray X is from downcomer 51 to weir 52, flow path f from downcomer 51 to weir 53 and flow path g from downcomer 54 to Weir 56. Similarly on tray Y flow path e is from downcomer 57 to weir 58, flow path 1 from downcomer 59 to weir 61 and flow path g from downcomer 59 to weir 62. On tray Z flow path e is from downcomer 63 to weir 64, flow path 7" from downcomer 63 to weir 66 and flow path g from downcomer 67 to weir 68.

For the flow on tray Z, the downcomer 63 is baflled as illustrated in FIGURES 10 and 11. Weirs 58 and 61 are baflled, also as shown in FIGURES 10 and 11. Downcomer 57 and weir 52 are unbafiled as shown in FIG- URE 9. Similarly, downcomers 54 and 67 and Weirs 62 and 64 are unbaffied while downcomers 51 and 59 are bafiled in the same manner as downcomer 63, Weirs 56 and 68 are bathed in the same manner as weir 58 and Weirs 53 and 66 are bafiled in the same manner as weir 61.

The following examples relate to the operation of a reboiled absorber of the type illustrated in FIGURE 3 of U.S. 2,984,988, Berger et al. (1961).

Example I In an example of a four-path column having valve trays without balancing, the dimensions are as shown in Table I. With conditions and feed as shown in Table H, the results shown in Table III are obtained.

Example II In an example of a four-path column having valve trays with balancing, the dimensions are as shown in Table IV. With feed and conditions as shown in Table V, the results shown in Table VI are obtained.

A comparison of Examples I and II reveals the advantages obtained by balancing a four-path column in obtaining balance conditions on each tray, thus reducing the tendency for column upset.

Example III In an example of a three-path column having sieve trays Without balancing, the dimensions are as shown in Table VII. With conditions and feed as shown in Table VIII, the results shown in Table IX are obtained.

Example IV In an example of a three-path column having sieve trays with balancing, the dimensions are as shown in Table X. With conditions and feed as shown in Table XI, the results shown in Table XII are obtained.

A comparison of Examples III and IV reveals advantages obtained by balancing a three-path column in obtaining balance conditions on each tray, thus reducing the tendency for column upset.

In Example I and Example III, it is assumed that balanced flow of fluid is attained across the various paths, and calculations demonstrate that such balanced conditions are not attained. This is illustrated by the fact of calculated values of pressure drop across different paths between the same location differ, when actually, of course, the drops must be equal. Similarly, calculated values of downcommer backup are different in the same downcomer are obvious inequity. Therefore, it is clear that balanced flow conditions are not achieved. In actual operation, a redistributing of flow occurs to reach equilibrium resulting in poor liquid vapor contact. In extreme cases, one path can have substantially all liquid while another path has substantially all vapor.

TABLE I Tray A and C Tray B and D Path 1) Path a Path b Path a Tray Spacing, 1n 24 24 24 24 Tower Diameter, ft. 12 50 .50 12 50 Tower Area, sq. ft 122 72 122.72 122 72 122.72 The following dimensions are for one-half Tray:

Downcomer area, sq. ft 8. 08 6. 01 8. 08 6. 01 Downcomer seal area, sq. ft 8. 08 6. 01 8. 08 6.01 Bubbling area, sq. ft 19. 04 14. 16 19. 04 14. 16 Free area, sq. ft 27. 12 20. 17 27. 12 20. 17 Min. area under Downcomer, sq. ft.- 2. 43 2. 16 2. 60 1. 53 Waste area, sq. ft 0 0 0 Overflow Weir length, in 149. 19 88. 34 140. 124. 56 Length of overflow Blanked Area, 111.- 0 0 0 Inlet Weir length, in 140 25 124. 51 149. 19 88. 34 Length of Inlet Blanked area, in" 0 0 0 0 Length of Flow Path, in 18 83 18. 83 18. 83 18. 83 Width of Flow ath, in.--- 129. 51 96. 32 129. 51 96. 32 Overflow Weir eight, in-.- 3. 00 3.00 3.00 3.00 Downcomer Clearance, in... 2. 50 2. 50 2. 50 2. 50 Inlet Weir Height, 111..-- 0 0 0 0 Valve Pitch 12. 00 12. 00 12. 00 12. 00 Number of Va1ves/Tray-. 228 170 228 170 TABLE II [Temperature 174 F., Pressure 300 p.s.i.a.]

Va or L1 old q Component:

Nitrogen. 0. 0. Carbon Dioxide 0. 0008 0. 0004 Methane 0. 0141 0. 0077 Ethane 0. 3079 0. 1681 Propane 0. 6197 0. 4346 Isobutane 0. 0258 0. 0319 35 n-Butane 0. 0266 0. 0420 lsopentane 0. 0019 0. 0058 n-Pentane 0. 0012 0. 0042 Heptane 0. 0003 0. 0028 M80 0. 0015 0. 3026 0. 9998 1. 0001 233, 274 430, 701 R 400 Rates Per Tray:

Density, lbs/cu. It 2. 168 33. 584 Viscosity, Centipoise. 0. 010 0. 143 Rate, c.i.s 50. 281 11. 320 gaze, \siullloadndulnnu- 13. 209

a e, g.p. sq. 1:. of 0.5.3 19, 51a

2, 394, 607 7, 315, 665 Rate, g.p m 5,

Paths b and c Paths a and d Trays A, B, 0, D Trays A, B, C, D

Vapor Liquid Vapor Liquid Rate, c.!.s 14. 418 Rate, V Load 3. 788 Rate, Std. g.p.d-- 685, 64 Rate, g.p.d-

Rate, g.p.m

TABLE III Trays A and C Trays B and D Paths Paths Paths Paths bande aandd bandc aandd Fliiorgng cheek: Fraction flood at design V/L a o Hydraulics:

Downcomer Back-Up 9. 980 9. 898 9. 848 10. 627 Dry Tray Pressure Drop- 1. 951 1.951 1.951 1. 951 Total Tray Pressure Drop 5. 360 6. 031 5. 523 5. 084 Pressure Drop through Min. Area Under Downeomer 1- 048 0. 734 0. 915 1. 462 Height of Liquid on Tray 3. 409 4. 081 3. 573 3. 133

Downeomer Residence Time, seconds Vapor Velocities, it./see. Bubbling Area...

Tray Eflicieney for the Key Components 0. 556 0. 615 0. 571 0. 528 Liquid Rates:

G.p.m./i.neh of Overflow Weir Length 9. 765 12. 264 10. 387 8. 698

G.p.m.linoh of Average Flow Path Width..-.- 11. 248 11. 248 11. 248 11. 248

Paths Paths Paths Paths bandc aandd bandc aandd Tray Spacing, in 24 24 24 24 Tower Diameter, it. 12. 50 12. 50 12. 50 12. 50 Tower area, sq. ft 122. 72 122. 72 122. 72 122. 72 The following dimensions are for one-half tray:

Downcomer area, sq. ft 8.32 6. 19 8. 32 6. 19 Downcomer seal area, sq. ft 8 32 6. 19 8. 32 6. 19 Bubbling area, sq. ft..." 18.53 13. 80 18. 53 13. 80 Free area, sq. it 22 36 24. 49 22.36 24. 49 Min. area under Downcomer, sq. ft. 2 44 1. 82 2.08 1. 55 Waste area, sq. it 0 0 0 Overflow Weir length, in 119 78 89. 17 140 45 104. 56 Length of Overflow Blanked Area, in 29 36 0 0 19. 74 Inlet Weir length, in 140 45 104. 56 119 78 89. 17 Length of Inlet Blanked Area, in. 0 19. 67 29 36 0 Length of Flow Path, in 18. 33 18.33 18 33 18. 33 Width of flow path, in 130.12 96. 87 130 12 96.87 Overflow Weir Height, i 3. 00 3. (l0 3 00 3. 00 Downcomer clearance, in. 2. 50 2. 50 2 50 2. 50 Inlet Weir height, in 0 0 0 0 Valve Pitch 12. 00 12. 00 12 00 12.00 Number of valves 222 166 2 1 6 TABLE V Vapor Liquid T L 11 g ge 0 008 0 004 AB E V ar on ioxi e 0. 0.

o. 0141 0. 0017 w umnData 0.30 9 0.1681 0- 0. Path 0 Path! Path g 0 Type tray, three path flow: 0266 0420 Tray Spacing, in 24 24 24 0019 0053 Tower diameter, it 9. 00 9. 00 9. 00 0012 0042 Tower area, sq. it 63. 62 63. 62 63. 62 0003 0028 Downcomer area, sq. it 1. 93 2. 49 1. 93 0015 3026 Downcomer seal area, sq. ft 1. 93 2. 49 1. 93 Bubbling area, sq. ft 15.48 19. 93 15. 48 9998 0001 Free area, sq. ft 17. 42 22.43 17. 42 274 430, 701 Min. area under Downcomer, sq. it.-." 2. 08 2.18 1.14 LR 400 Area under Splash Baflie, sq. It 0 0 0 Rat r m Waste Area, sq. ft; 0 o 0 Dens1ty,lhS./9l1. it..- 2- 168 534 Hole Area, sq tt 1. 55 1. 99 1. 55 iscosi y, cenhpmsefl 010 0-143 Percent Hole Are 10.00 10.00 10.00 320 Hole Diameter, in. 1. 000 1. 006 1. 000 Tray thickness, in 0.1345 0. 1345 0. 1345 Overflow Weir Height, 3.00 3. 0O 3. 00 Overflow Weir Length, in 54. 93 104. 61 100. 61 Length of Overflow Blanked area, 0 0 0 7,315,655 Inlet weir height, ln 0 0 0 080 inletggeiif' llelrligtlfllirlifiga 100.61 104 61 54. 93 eng 0 et a e area, in- 0 O 0 Paths b and c Paths a and b Length of Flow path, 26.86 26. 86 26.86 Trays A, B, C, D Trays A, B, C, D Width of flow path, 71.17 105. 74 17. 17 Hole spacing, inches 3. 01 3. 01 3. 01

Vapor Liquid vapor Liquid Smooth side of tray up Hole Arrangement 245 10 729 415 Equllateral T g e 318 1 Does not include any blanked area.

TABLE VI Trays A and C Trays B and D Paths Paths Paths Paths bandc aandd bandc aandd Flooding check: Fraction Flood at Design V/L Height of Liquid on Tray Downcomer Residence Time, seconds 5. 129 5.129 5. 129 5. 129 Vapor Velocities, it. see. Bubbling Area. 0. 778 0. 778 0.778 0.778 Tray Efliciency for the key Components 0. 609 0. 609 0. 567 0. 567 Liquid Rates:

G.p.m./inch of Overflow Weir Length 12.157 12. 157 10. 367 10.367

G.p.m./inch of Average Flow Path Width 11.191 11. 191 11. 191 11. 191

TABLE VIII Path 1 Path 2 Path 3 Vapor Liquid Vapor Liquid Vapor Liquid Component:

Propylene .0005 0.0003 0 .0005 0 .0003 0 .0005 0 .0003 Propane- 0 .0009 0 .0005 0 .0009 0 .0005 0 .0009 0 .0005 Isobutane.- 0 .0247 0 .0160 0 .0247 0 .0160 0 .0247 0 .0160 0.0290 0.0190 0.0290 0.0190 0 0290 0.0190 0 .0226 0 .0151 0 .0226 0 .0151 0 .0226 0 .0151 0 .0542 0 .0370 0 .0542 0 .0370 0 .0542 0 .0370 0 .0435 0 .0297 0 .0435 0 .0297 0 .0435 0 .0397 0 .1418 0 .1079 0 .1418 0 .1079 0 .1418 0 .1079 0 .3318 0 .2619 0 .3318 0 .2619 0 .3318 0 .2619 0 .0308 0 .0245 0 .0308 0 .0245 0 .0308 0 .0245 Methyleyclohexane 0 .3202 0 .4880 0 .3202 0 .4880 0 .3202 0 .4880

Total 1 .0000 0 .9999 1 .0000 0 .9999 1 .0000 0.9999 Mols 28, 561 47, 906 36, 778 01, 688 28, 561 906 LR 0 .900 9 .900 Rates Per Tray:

Density, lbs/cu. ft 2.212 Viscosity, centipoise- 0.011 Rat c.f.s 11 .518 Rate, V Load 3 .122 Rate, Std. g p.d. 387, 910 6 098 Flooding cheek, Path a Safety Factor Vapor Vapor Load, Load Flood/Design (1) Design Load 3. 122 (2) Jet flood at Max. Design Liquid Load 4. 242 1. 359 (3) Jet Flood at Design V/L Ratio--. 3. 648 1. 169 (4) Flooding by Blowing 9. 365 3. 000 (5) Flooding by System Limitation 3. 408 1. 092

Hydraulics Path e Path 1' Path g Downcomer Back-Up 8. 283 7. 526 7. 612 Dry Tray Pressure Drop 0. 961 1. 004 1. 025 Total Tray Pressure Drop 4. 487 4. 061 3. 873 Pressure drop through Downcomer Seal. 0. 269 0. 407 0.891 Height oi Liquid on Tray 3. 527 3. 057 2. 848 Downcomer Residence Time, seconds 2. 736 2. 730 2. 736 Liquid Rates:

G.p.m./inch 0t Overflow Weir Length 11. 558 7. 815 6. 311 G.p.m.linch of Average Flow Path Width 8. 164 7. 732 8. 164

Flooding cheek, Path 1 Flooding check, Path g Safety Factor Safety Factor Vapor Liquid Load, Vapor Load, Vapor Liquid Load, Vapor Load Load cu. it.lsee. Flood/Design Load cu. ft./sec. Flood/Design SIEVE TRAY, CAPACITY CHECK Vapor Velocities, ft.lsec..- Path e Path I Path g Bubbling area 0. 744 0. 744 0. 744 Hole area 7. 441 7. 442 7. 441 Tray Efficiency for the Key 0. 837 800 782 TABLE X Sieve Tray Column Data Path e Path 1 Path g Tray Spacing, in 24 24 24 Tower Diameter, 5 9. 00 9. 00 9. 00 Tower Area, sq. ft. 63. 62 63. 62 63. 62 Downoomer Area, 1. 93 2. 49 1. 93 0 Downcomer Seal Area, sq. 1. 93 2. 49 1. 93 Bubbling area, sq. it---- 15. 48 19. 93 15. 48 Free Area, sq. it 17. 42 22. 43 17. 42 Min. Area Under Downcomer, q. 1. 14 1. 47 1. 14 Area Under Splash Battle, sq. it--. 0 0 0 Waste Area, sq. ft 0 0 0 Hole Area, sq ft... 1. 55 1. 99 1. 55 Percent Hole Area 10. 00 10. 00 10. 00 Hole Diameter, in 1. 000 1. 000 1. 000 Tray Thickness, in 0. 1345 0. 1345 0.1345 Overflow Weir Height, in 3. 00 3. 00 3. 00 Overflow Weir Length, in. 54.93 70. 73 54. 93 Length 01 Overflow Blanked Area, 0 33. 88 45. 68 Inlet Weir Height, in 0 0 0 Inlet Weir Length, in. 54.93 70.73 54. 93 70 Length of Inlet Blanked Area, in 45. 68 33. 88 0 Length of Flow Path, in 26. 86 26.86 26. 86 Width of Flow Path, in 77. 77 105. 74 77. 77 Hole Spacing, inches.-. 3. 01 3.01 3. 01 Smooth side of Trey Up Hole Arrangement Equilateral Triangle 1 Does not include any blanked area. 75

TABLE XI [Temperature, 347 F., Pressure 200 p.s.i.a.]

Path e Path f Path g Vapor Liquid Vapor Liquid Vapor Liquid Component:

. 0.0003 0 .0005 0 .0003 0 .0005 0 .0003 0 .0005 0 .0009 0 .0005 0 .0009 0 .0005 0 .0160 0 .0247 0 .0160 0 .0247 0 .0160 l-butene... 0.0290 0 .0190 0 .0290 0 .0190 0 .0290 0 .0190 11-13 utane. 0 .0226 0 .0151 0 .0226 0 .0151 0 .0226 0 .0151 t-Butene-2 0 .0542 0.0370 0.0542 0.0370 0 .0542 0 .0370 c-Butene-2 0 .0435 0 .0297 0 .0435 0 .0397 0 .0435 g Rates Per Tray:

Density, lbs/cu. it Viscosity, centipoiseate, c.i.s Rate, V Load- Rate, Std. g.p.d Rate, Std. g.p.d./Sq. Ft. 0! c.s.a Rate, g.p.d Rate, 2 p m TAB LE XII Flooding Check, Path 6 Liquid Load,

Safety Factor Vapor Load (1) Design Load 3. 122 (2) Jet Flood at Max. Design Liquid Load. 4. 242 (3) Jet Flood at Design V/L Ratio 3. 648

(4) Flooding by Blowing (5) Flooding by System Limitation 3. 408

Hydraulics Path e Downcomer Back-Up.

Pressure Drop Through Downco Height of Liquid on Tray a. 527 I Downcomer Residence Time, seoon 2. 736 2. 736 2. 736 Liquid Rates:

G.p.m./inch oi Overflow Weir Length 11. 558 11. 559 11. 558 G.p.m./lnch of Average Flow Path Wid 8. 164 7. 732 8. 164

Flooding Check, Path i Safety Factor Liquid Load, Vapor Load, Vapor Load cu. it./sec. Flood/Design Vapor Velocities, it./sec Path 0 Path i Path g Bubbling area-.- 0. 744 0. 744 0. 744 Hole Area 7. 441 7. 442 7. 441 Tray Efficiency for the Key Components 0. 837 836 837 I claim: 1. A fractional distillation column comprising:

a plurality of three-path vapor-liquid contact trays hav- 6 ing two zones of unequal area;

a first downcomer for each tray feeding on the perimeter thereof;

a second downcomer for each tray parallel with said first downcomer spaced from the perimeter of said unequal areas;

said first and second downcomers being spaced to provide equal flow paths on each of said trays;

baflle means on each side of said second downcomer, said bafile means having a plurality of separate flow openings spaced along said bafiie means and proportional to the zones of unequal area being fed by said second downcomer to obtain distribution of the liquid in proportion to the two areas of said zones over which it flows;

a first weir on each of said trays to regulate flow into a corresponding first downcomer for the next lower y;

second and third weirs on each of said trays to regulate flow with a corresponding second downcomer for said next lower tray; and

baflle means on said second and third weirs, said baffle means having a plurality of separate flow openings spaced along said baffle means to fix the ratio of the eifective lengths thereof to provide the desired height of liquid on the flow paths of said trays.

2. A fractional distillation column comprising:

a plurality of first four-path vapor-liquid contact trays having zones of unequal areas;

a pair of first horizontally elongated parallel downcomers for each of said first vapor-liquid contact trays, spaced to distribute liquid over four equal flow paths on each of said first trays, each of said first downcomers being positioned above two zones of unequal area and distributing liquid to said two zones having unequal areas;

a plurality of second four-path vapor-liquid contact trays alternately spaced between said first trays;

a pair of second horizontally elongated parallel downcomers for each of said second trays parallel in vertical projection with said first downcomers feeding on the perimeter thereof;

a centrally located third horizontally elongated downcomer for each of said second trays, parallel with said second downcomer;

baflie means on each of said first downcomers, said baflle means having a plurality of separate flow openings spaced along said baflle means and proportional to the zones of unequal area being fed by said second downcomers to eflect distribution of the liquid in proportion to the areas of the zone over which it flows;

a pair of first overflow weirs on each of said second trays positioned to regulate flow of liquid from said 14 second trays into each corresponding first downcomer;

a second overflow weir on each of said first trays to regulate flow of liquid from said first trays into each corresponding second downcomer; and

a pair of third overflow weirs on each of said first trays to regulate flow of liquid from said first trays into corresponding third downcomers.

3. The distillation column of claim 2 including baflle means on said third downcomers providing the desired height of liquid therein and maintaining equal eflective lengths on the sides thereof;

bajfie means on each pair of said first weirs to fix the ratio of efiective lengths thereof to provide the desired height of liquid on the flow paths on said second trays; and

bafiie means on each pair of said third overflow weirs to provide the desired height of the liquid on the flow paths of said first tray.

References Cited UNITED STATES PATENTS RONALD R. WEAVER, Primary Examiner.

US. Cl. X.R. 

